CN120083577B - Coupling type thermodynamic cycle system - Google Patents
Coupling type thermodynamic cycle systemInfo
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- CN120083577B CN120083577B CN202510586059.1A CN202510586059A CN120083577B CN 120083577 B CN120083577 B CN 120083577B CN 202510586059 A CN202510586059 A CN 202510586059A CN 120083577 B CN120083577 B CN 120083577B
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F01—MACHINES OR ENGINES IN GENERAL; ENGINE PLANTS IN GENERAL; STEAM ENGINES
- F01K—STEAM ENGINE PLANTS; STEAM ACCUMULATORS; ENGINE PLANTS NOT OTHERWISE PROVIDED FOR; ENGINES USING SPECIAL WORKING FLUIDS OR CYCLES
- F01K23/00—Plants characterised by more than one engine delivering power external to the plant, the engines being driven by different fluids
- F01K23/02—Plants characterised by more than one engine delivering power external to the plant, the engines being driven by different fluids the engine cycles being thermally coupled
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F01—MACHINES OR ENGINES IN GENERAL; ENGINE PLANTS IN GENERAL; STEAM ENGINES
- F01K—STEAM ENGINE PLANTS; STEAM ACCUMULATORS; ENGINE PLANTS NOT OTHERWISE PROVIDED FOR; ENGINES USING SPECIAL WORKING FLUIDS OR CYCLES
- F01K13/00—General layout or general methods of operation of complete plants
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Abstract
The invention discloses a coupling type thermodynamic cycle system, which relates to the technical field of energy application, and effectively realizes the coupling of an organic Rankine cycle module and a Brayton cycle module in fusion reactor heat source application by inputting an expanded first working medium and a deoxidized second working medium into a heat exchanger module for heat exchange, so that the temperature of the first working medium can be reduced through heat transfer to reduce the cooling cost of the first working medium, and the heat in the Brayton cycle module can be utilized to reduce the waste heat. In addition, the organic Rankine cycle module is provided with a reheating stage, and can effectively improve the energy conversion efficiency of the coupled thermodynamic cycle system. And, the parameter of the coupled thermodynamic cycle system can further improve the system thermal efficiency based on the enthalpy value setting.
Description
Technical Field
The invention relates to the technical field of energy application, in particular to a coupling type thermodynamic cycle system.
Background
Compared with non-dispatchable renewable energy sources such as wind energy, photovoltaic power generation and the like, fusion energy is almost inexhaustible due to fuel, and has the prospect of large-scale power generation as a dispatchable energy source.
In the power generation process, the thermodynamic cycle is a bridge for connecting heat energy and electric energy, and the reasonable thermodynamic cycle can effectively improve the energy utilization efficiency. However, heat generated by the fusion reactor is accompanied by a high-temperature and high-pressure environment, and a large amount of waste heat is not utilized when the conventional thermodynamic cycle is applied to the fusion reactor, so that the wide application and development of fusion energy as a power generation energy source are severely restricted.
Disclosure of Invention
The embodiment of the invention aims to provide a coupled thermodynamic cycle system, which can fully utilize the heat energy of a fusion reactor and low-grade waste heat generated in the power generation process by coupling a Brayton cycle and an organic Rankine cycle, reduces the waste heat generated by the whole system and has good thermal performance.
The embodiment of the invention provides a coupled thermodynamic cycle system, which comprises a Brayton cycle module, a heat exchanger module and an organic Rankine cycle module with a reheating stage, wherein the heat exchanger module comprises a first channel and a second channel;
The working medium of the Brayton cycle module is a first working medium, and the working medium of the organic Rankine cycle module is an organic second working medium;
The Brayton cycle module is connected with the heat source and used for converting heat energy transferred by the heat source into first electric energy; the inlet of the first channel sucks a first working medium expanded by the Brayton cycle module, the inlet of the second channel sucks a second working medium deoxidized by the organic Rankine cycle module, the outlet of the first channel and the outlet of the second channel respectively return the first working medium and the second working medium after heat exchange to the Brayton cycle module and the organic Rankine cycle module, and the organic Rankine cycle module is used for converting heat energy transferred by the heat exchanger module into second electric energy.
As an improvement of the scheme, the first working medium is supercritical carbon dioxide, and the second working medium is R245fa.
As an improvement of the scheme, the brayton cycle module comprises a first turbine unit, a regenerator, a cooler unit, a compressor unit and a first generator;
the heat source is connected with the inlet of the first turbine unit, the outlet of the first turbine unit is connected with the inlet of the heat regenerator, the inlet of the first generator and the inlet of the first channel, the first outlet of the heat regenerator is connected with the heat source, the second outlet of the heat regenerator is connected with the inlet of the compressor unit through the cooler unit, and the outlet of the compressor unit is connected with the heat regenerator and the inlet of the first turbine unit.
The first working medium sequentially passes through the compressor unit, the first turbine unit, the heat regenerator and the cooler unit and then is introduced into the compressor unit to form circulation, and the first working medium output through the outlet of the first channel sequentially passes through the heat regenerator and the cooler unit and is introduced into the compressor unit.
As an improvement of the above scheme, the compressor unit comprises a cooler and a plurality of compressors connected in sequence, and the cooler is also arranged between the adjacent compressors.
As an improvement of the scheme, the first turbine unit comprises a first high-pressure turbine and a first low-pressure turbine which are sequentially connected, wherein the inlet of the first high-pressure turbine is the inlet of the first turbine unit, and the outlet of the first low-pressure turbine is the outlet of the first turbine unit.
As an improvement of the above-mentioned scheme, the organic rankine cycle module includes a second turbine unit, a reheater, a condenser, a deaerator, a mixer unit, a steam extraction pipeline unit, and a second generator;
The second turbine unit comprises a second high-pressure turbine and a second low-pressure turbine, the mixer unit comprises a first mixer, a second mixer and a third mixer, and the steam extraction pipeline unit comprises a first steam extraction pipeline, a second steam extraction pipeline and a third steam extraction pipeline;
The outlet of the second channel is connected with the inlet of the second high-pressure turbine, the outlet of the second high-pressure turbine is connected with the inlet of the second low-pressure turbine and the inlet of the reheater, the outlet of the reheater is connected with the inlet of the second low-pressure turbine, the outlet of the second low-pressure turbine is connected with the inlet of the second generator and the inlet of the condenser, the outlet of the condenser is connected with the inlet of the first mixer, the outlet of the first mixer is connected with the second mixer, the outlet of the second mixer is connected with the inlet of the deaerator, the outlet of the deaerator is connected with the inlet of the third mixer, the outlet of the third mixer is connected with the inlet of the deaerator and the inlet of the second channel, the first steam extraction pipeline connects the second high-pressure turbine with the third mixer and the reheater, the second steam extraction pipeline connects the second low-pressure transmission with the first mixer, and the third steam extraction pipeline connects the second low-pressure turbine with the second mixer.
The improvement of the scheme is that the second working medium sequentially passes through the deaerator, the third mixer, the heat exchanger module, the second high-pressure turbine, the reheater, the second low-pressure turbine, the condenser, the first mixer and the second mixer and then is introduced into the deaerator to form circulation, the second working medium also enters the third mixer and the reheater through the second high-pressure turbine, and the second working medium also is respectively introduced into the first mixer and the second mixer through the second low-pressure turbine.
The organic Rankine cycle module further comprises a power unit, wherein the power unit comprises a first pump and a second pump;
the first pump is arranged between the outlet of the condenser and the inlet of the first mixer, and the second pump is arranged between the outlet of the deaerator and the inlet of the third mixer.
As an improvement of the above aspect, the organic rankine cycle module further includes a valve unit including a first valve, a second valve, a third valve, and a fourth valve;
The first valve is arranged between the outlet of the second channel and the inlet of the second high-pressure turbine, the second valve is arranged between the outlet of the second mixer and the inlet of the first mixer, the third valve is arranged between the outlet of the third mixer and the inlet of the deaerator, and the fourth valve is arranged between the outlet of the third mixer and the inlet of the second channel.
Compared with the prior art, the coupling type thermodynamic cycle system disclosed by the invention has the advantages that the expanded first working medium and the deoxidized second working medium are input into the heat exchanger module for heat exchange, so that the coupling of the organic Rankine cycle module and the Brayton cycle module is effectively realized, the temperature of the first working medium can be reduced through heat transfer, the cooling cost of the first working medium is reduced, the heat in the Brayton cycle module can be utilized, and the waste heat is reduced. In addition, the organic Rankine cycle has a reheating stage, which can effectively improve the energy conversion efficiency of the coupled thermodynamic cycle system.
Drawings
FIG. 1 is a schematic diagram of a coupled thermodynamic cycle system according to an embodiment of the present invention;
FIG. 2 is a schematic diagram of a Brayton cycle module according to an embodiment of the present invention;
FIG. 3 is a schematic diagram of a further brayton cycle module provided in accordance with an embodiment of the invention;
Fig. 4 is a schematic structural diagram of an organic rankine cycle according to an embodiment of the present invention.
Detailed Description
The following description of the embodiments of the present invention will be made clearly and completely with reference to the accompanying drawings, in which it is apparent that the embodiments described are only some embodiments of the present invention, but not all embodiments. All other embodiments, which can be made by those skilled in the art based on the embodiments of the invention without making any inventive effort, are intended to be within the scope of the invention.
In the description of the specification and claims, it should be understood that the terms first, second, etc. are used solely for the purpose of distinguishing between similar features and not necessarily for the purpose of describing a sequential or chronological order, and not necessarily for the purpose of indicating or implying a relative importance or implicitly indicating the number of features indicated. The terms are interchangeable where appropriate. Thus, a feature defining "a first" or "a second" may explicitly or implicitly include at least one such feature.
Because fusion reactors have the characteristics of high temperature and high pressure, the brayton cycle or the rankine cycle is generally adopted when the fusion reactor is used for energy conversion and power generation. However, the problems of the prior art are at least that the brayton cycle and the rankine cycle cannot well utilize low-grade waste heat, so that the heat energy utilization efficiency in the power generation process is low, and a large amount of loss is caused.
Based on the above considerations, the embodiments of the present invention provide a coupled thermodynamic cycle system. Referring to fig. 1, in the present embodiment, the coupled thermodynamic cycle system includes a brayton cycle module 1, a heat exchanger module 2, and an organic rankine cycle module 3 with a reheat stage, wherein the heat exchanger module includes a first passage and a second passage;
the working medium of the Brayton cycle module 1 is a first working medium, and the working medium of the organic Rankine cycle module 3 is an organic second working medium;
The Brayton cycle module 1 is connected with a heat source and used for converting heat energy transferred by the heat source into first electric energy, an inlet of a first channel sucks first working medium expanded by the Brayton cycle module, an inlet of a second channel sucks second working medium deoxidized by the organic Rankine cycle module 3, an outlet of the first channel and an outlet of the second channel respectively return the first working medium and the second working medium subjected to heat exchange to the Brayton cycle module 1 and the organic Rankine cycle module 3, and the organic Rankine cycle module 3 is used for converting heat energy transferred by the heat exchanger module 2 into second electric energy.
The Brayton cycle module can carry out energy cycle conversion on heat energy generated by the fusion reactor in a high-temperature and high-pressure environment to generate electric energy. However, it can be appreciated that the conventional brayton cycle requires cooling of its working medium during operation, and a large amount of heat energy is lost during cooling, thereby greatly reducing the efficiency of heat energy utilization.
According to the embodiment of the invention, the expanded first working medium and the deoxidized second working medium are input into the heat exchanger module for heat exchange, so that the coupling of the organic Rankine cycle module and the Brayton cycle module in fusion reactor heat source application is effectively realized, the temperature of the first working medium can be reduced through heat transfer, the cooling cost of the first working medium is reduced, the heat in the Brayton cycle module can be utilized, and the waste heat is reduced. In addition, the organic Rankine cycle module is provided with a reheating stage, and can effectively improve the energy conversion efficiency of the coupled thermodynamic cycle system. The parameters of the coupled thermodynamic cycle system can further improve the thermal efficiency of the system based on the enthalpy setting.
The traditional Rankine cycle uses water as a working medium, the thermodynamic cycle is that the water is heated into high-temperature high-pressure water vapor in a boiler, the water vapor enters a steam turbine to expand and do work, and a rotor of the steam turbine is pushed to rotate, so that a generator is driven to generate electricity. The exhaust steam after doing work enters a condenser, is cooled and condensed into water, and is pumped back to the boiler by a water supply pump, so that one cycle is completed. It will be appreciated that water is not suitable for use as a heat source in the low temperature range, as it cannot evaporate at lower temperatures. The organic second working medium is used in the organic Rankine cycle module provided by the embodiment of the invention, and can be used for energy conversion of low-grade waste heat.
It should be further noted that, as the service life of the conventional heat exchanger module increases, temperature slip may occur, which may further reduce the thermal efficiency of the thermodynamic cycle system. Considering that temperature curves of an organic Rankine cycle module and a Brayton cycle in the prior art are difficult to match efficiently, the embodiment of the invention provides enthalpy change setting according to a first working medium and a second working medium when parameter setting of a coupling thermodynamic cycle system is carried out. The organic rankine cycle module includes a pump for pumping the second working fluid. And calculating the power of the pump according to the quality and enthalpy change condition of the second working medium under the pump connecting line. The system thermal efficiency can be improved by setting parameters of the coupling thermodynamic cycle system under the enthalpy change condition, and Yong loss is prevented from being increased.
As a preferred embodiment, the first working medium is supercritical carbon dioxide, and the second working medium is R245fa.
It should be noted that, the brayton cycle module with the working medium of supercritical carbon dioxide is typically operated at 500-700 ℃, and the organic rankine cycle module with the working medium of R245fa is typically operated at a temperature below 200 ℃.
In the embodiment of the invention, water, toluene and R245fa are respectively selected as the second working medium to carry out the thermal performance analysis of the system, and the analysis is shown in table 1.
TABLE 1 thermal properties corresponding to different second working fluids
It can be seen that R245fa can operate at lower pressures and has a lower boiling point than water or toluene. In the embodiment of the invention, the operating conditions of the organic Rankine cycle module in the coupled thermodynamic cycle system are comprehensively considered, and R245fa is preferably used as the second working medium.
As a preferred embodiment, referring to fig. 2, the brayton cycle module 1 includes a first turbine unit 11, a regenerator 12, a cooler unit 13, a compressor unit 14, and a first generator 15;
The heat source is connected with the inlet of the first turbine unit 11, the outlet of the first turbine unit 11 is connected with the inlet of the heat regenerator 12, the first generator 15 and the inlet of the first channel, the first outlet of the heat regenerator 12 is connected with the heat source, the second outlet of the heat regenerator 12 is connected with the inlet of the compressor unit 14 through the cooler unit 13, and the outlet of the compressor unit 14 is connected with the heat regenerator 12 and the inlet of the first turbine unit 11.
In the above scheme, the first turbine unit 11 performs expansion work by using a heat source, converts thermal energy into mechanical energy, and drives the first generator 15 to generate electricity, so as to realize energy conversion. The regenerator 12 recovers waste heat from the first turbine unit 11 and inputs a part of the residual heat into the compressor unit 14, and sends another part of the residual heat to the regenerator for reheating, thereby improving the thermal efficiency of the whole cycle. The cooler unit 13 ensures the normal operation of the compressor unit 14 by cooling down. The compressor unit 14 achieves energization by doing work in preparation for subsequent expansion work. By adopting the brayton cycle module 1 provided by the embodiment of the invention, the expansion work, waste heat recovery, cooling and compression processes can be repeated continuously, so that continuous circulation is formed, and energy conversion and power generation are realized continuously.
The embodiment of the invention provides a structural schematic diagram of the brayton cycle module shown in fig. 2 and 3. The dashed line portions in fig. 2 and 3 are flow paths of the first working medium, and the first working medium circularly flows in the brayton cycle module.
In some preferred embodiments of the present invention, the temperature and/or pressure at each node in the brayton cycle module is pre-selected to accurately set specific parameters of the coupled thermodynamic cycle system. The selected temperature and/or pressure requirements meet the operating temperatures and/or pressures of the brayton cycle module and the organic rankine cycle module.
Illustratively, the preselected temperature includes an outlet temperature of 270 ℃ for the first turbine unit, an inlet temperature of 210 ℃ for the regenerator, an outlet temperature of 130 ℃ for the regenerator, a pressure of 8.65 megapascals, a thermal power of 300 kilowatts, and an inlet temperature of 32 ℃ for the compressor unit. An initial enthalpy change is obtained based on the set temperature and/or pressure for parameter design.
Further, preferably, the first working medium sequentially passes through the compressor unit 14, the first turbine unit 11, the regenerator 12 and the cooler unit 13, and then is introduced into the compressor unit 14 to form circulation, and the first working medium output through the outlet of the first channel sequentially passes through the regenerator 12 and the cooler unit 13 and is introduced into the compressor unit 14.
In the embodiment of the invention, the first working medium flows orderly among different components, so that the system is more flexible in energy distribution.
Preferably, referring to fig. 3, the compressor unit 14 includes a cooler and a plurality of compressors connected in sequence, and a cooler is further disposed between adjacent compressors.
Further, in some preferred embodiments, the compressors include a first compressor 141, a second compressor 142, and a third compressor 143 connected in sequence, and the coolers include a first cooler 144 and a second cooler 145. Wherein the first cooler 144 is provided between the first compressor 141 and the second compressor 142, and the second cooler 145 is provided between the second compressor 142 and the third compressor 143. The inlet of the first compressor 141 is the inlet of the compressor unit 14, and the outlet of the third compressor 143 is the outlet of the compressor unit 14.
The temperature after each stage of compression can be reduced by arranging the cooler between the adjacent compressors, so that irreversible loss in the compression process is reduced, and the compression efficiency is improved. And the multistage compressor can flexibly adjust the compression ratio and the flow according to different working conditions.
In the embodiment of the present invention, two flow paths exist between adjacent compressors, namely, a flow path from an upper compressor directly to a lower compressor and a flow path from the upper compressor to the lower compressor through a cooler. In fig. 3 of the embodiment of the present invention, the different loops are represented by solid lines and dashed lines, where the solid lines or the dashed lines correspond to the actual physical connection relationship in actual operation.
Preferably, the first turbine unit 11 includes a first high-pressure turbine 111 and a first low-pressure turbine 112 connected in sequence, the inlet of the first high-pressure turbine 111 is the inlet of the first turbine unit 11, and the outlet of the first low-pressure turbine 112 is the outlet of the first turbine unit 11.
The two-stage expansion is used for enabling the first working medium to expand and do work step by step in different pressure stages, so that the energy of the high-temperature high-pressure working medium is fully utilized, and the heat energy is more efficiently converted into mechanical energy.
As a preferred embodiment, referring to fig. 4, the organic rankine cycle module 3 includes a second turbine unit, a reheater 32, a condenser 33, a deaerator 34, a mixer unit, a steam extraction pipe unit, and a second generator 37;
The second turbine unit comprises a second high-pressure turbine 311 and a second low-pressure turbine 312, the mixer unit comprises a first mixer 351, a second mixer 352 and a third mixer 353, and the steam extraction pipeline unit comprises a first steam extraction pipeline 361, a second steam extraction pipeline 362 and a third steam extraction pipeline 363;
the outlet of the second channel is connected with the inlet of the second high-pressure turbine 311, the outlet of the second high-pressure turbine 311 is connected with the inlet of the second low-pressure turbine 312 and the inlet of the reheater 32, the outlet of the reheater 32 is connected with the inlet of the second low-pressure turbine 312, the outlet of the second low-pressure turbine 312 is connected with the inlet of the second generator 37 and the inlet of the condenser 33, the outlet of the condenser 33 is connected with the inlet of the first mixer 351, the outlet of the first mixer 351 is connected with the second mixer 352, the outlet of the second mixer 352 is connected with the inlet of the first mixer 351, the outlet of the second mixer 352 is connected with the inlet of the deaerator 34, the outlet of the deaerator 34 is connected with the inlet of the third mixer 353, the outlet of the third mixer 353 is connected with the inlet of the second channel, the first extraction pipeline 361 connects the second high-pressure turbine 311 with the third mixer 353 and the reheater 32, the second extraction pipeline 362 is connected with the second low-pressure turbine 312 and the first mixer 351, and the third extraction pipeline 363 is connected with the second low-pressure turbine 352.
It should be noted that different reheat and extraction settings of the orc module can have a significant impact on the thermal performance of the system. And, even though the reheat phase is the same, the high/low pressure turbine's regenerative configuration and position will change the thermal performance of the power conversion system.
In the above preferred embodiment of the present invention, the organic rankine cycle module realizes two-stage expansion through the second high-pressure turbine and the second low-pressure turbine, and a reheater is provided between the two-stage expansion, so that the quality of the second working medium can be effectively improved, and the temperature of the second working medium entering the second low-pressure turbine is improved, so that the enthalpy drop of expansion work in the second low-pressure turbine is increased, and the mechanical work output and the energy utilization efficiency are improved.
It should be further noted that, in the conventional rankine cycle module, water is used as the second working medium, and a steam-water separator is also required to be configured in the system, so that energy conversion efficiency is reduced. The organic second working medium adopted by the scheme of the application does not contain moisture or water drops, so that a steam-water separator is not required to be arranged.
In addition, the steam extraction pipeline unit provided by the embodiment of the invention can effectively optimize the organic Rankine cycle module.
The organic Rankine cycle module has three times of steam extraction. And the first extraction steam extracts the second working medium from the second high-pressure turbine, and the second working medium enters the third mixer and the reheater to realize the step utilization of energy. The second working medium is extracted from the second low-pressure turbine by the second extraction steam and the third extraction steam and respectively enters the second mixer and the third mixer, so that the load can be flexibly adjusted, and the pressure and the temperature of the organic Rankine cycle module can be balanced.
In the embodiment of the present invention, preferably, the second working medium sequentially passes through the deaerator 34, the third mixer 353, the heat exchanger module 2, the second high-pressure turbine 311, the reheater 32, the second low-pressure turbine 312, the condenser 33, the first mixer 351 and the second mixer 352, and then passes through the deaerator 34 to form a circulation, the second working medium also passes through the second high-pressure turbine 311 to enter the third mixer 353 and the reheater 32, and the second working medium also passes through the second low-pressure turbine 312 to be respectively passed through the first mixer 351 and the second mixer 352.
Preferably, the organic Rankine cycle module 3 further comprises a power unit, wherein the power unit comprises a first pump 381 and a second pump 382;
the first pump 381 is provided between the outlet of the condenser 33 and the inlet of the first mixer 351, and the second pump 382 is provided between the outlet of the deaerator 34 and the inlet of the third mixer 353.
The power unit can ensure continuous circulation flow of the second working medium in the system, so that continuous conversion of energy is realized. The first pump is disposed adjacent the condenser and is capable of allowing liquid material exiting the condenser to be drawn into the pump at a minimum distance and with a minimum of resistance. The pipeline resistance loss is reduced, the energy consumption of the pump is reduced, and the system efficiency is improved. In the embodiment of the invention, the position of the pump in the power unit can meet the flow requirement of the second working medium, and the layout and the equipment installation space of the organic Rankine cycle module are fully considered.
In some preferred embodiments, the second working fluid enters the orc module through the power unit. It should be noted that, in consideration of the utilization rate and energy saving, not every pump of the power unit draws the second working medium from the outside to enter the circulation, and only a part of pumps may be selected as the working medium inlets.
In other preferred embodiments, the organic rankine cycle module may be pre-charged with the second working medium, and the second working medium existing in the cycle may be used to perform thermal energy conversion during operation.
Preferably, the organic rankine cycle module further comprises a valve unit comprising a first valve 391, a second valve 392, a third valve 393, and a fourth valve 394;
The first valve 391 is disposed between the outlet of the second passage and the inlet of the second high pressure turbine 311, the second valve 392 is disposed between the outlet of the second mixer 352 and the inlet of the first mixer 351, the third valve 393 is disposed between the outlet of the third mixer 353 and the inlet of the deaerator 34, and the fourth valve 394 is disposed between the outlet of the third mixer 353 and the inlet of the second passage.
By adjusting the opening of the valve in the valve unit, the flow of the second working medium between the components of the system can be accurately controlled, and the pressure of the components can be maintained within a preset range. The valve parameters are set by combining the design pressure and the safety requirement of the organic Rankine cycle module so as to ensure that the system can perform timely and effective safety protection.
It should be noted that, in the preferred embodiment of the present invention, the second working fluid flows out of the second mixer 352, flows to the first mixer 351 through the second valve 392, and is mixed with the second working fluid extracted from the second extraction conduit 362, and then flows into the deaerator 34 again through the second mixer 352.
It will be appreciated that the parameter design of the coupled thermodynamic cycle system is as important as the architecture design, and the above embodiment has described that the parameter of the coupled thermodynamic cycle system is set according to the enthalpy change of the first working medium and the second working medium in the present invention. More specifically, the heat exchange device is set according to enthalpy changes generated before and after the first working medium and the second working medium pass through each part, and the change of heat capacity flow rate can be fully considered in the process, so that the problem of heat efficiency reduction caused by temperature slippage of the heat exchanger module is avoided.
For a better understanding and implementation of the embodiments of the present invention, a configuration method of a coupled thermodynamic cycle system will be given below in conjunction with the system structure shown in the drawings of the present invention.
The embodiment of the invention provides a configuration method of a coupled thermodynamic cycle system, which is applied to the coupled thermodynamic cycle system, and comprises the following steps:
according to the structure of the coupled thermodynamic cycle system and the selection of working media, thermodynamic modeling is carried out to obtain a thermodynamic simulation model;
calculating enthalpy change of working medium passing through each component based on thermodynamic performance in the thermodynamic simulation model to obtain performance indexes of each component, wherein the performance indexes comprise power and efficiency;
performing preliminary configuration and verification on the thermodynamic simulation model according to the performance index to obtain a verification result;
and generating an optimal configuration scheme according to the verification result, and configuring the coupled thermodynamic cycle system by adopting the optimal configuration scheme.
In the process of establishing and solving the thermodynamic simulation model, the law of conservation of mass, the law of conservation of energy and the law of thermodynamics are required to be followed. The embodiment of the invention also takes the change of the enthalpy value into consideration.
In some preferred embodiments, it is possible to obtain from the law of conservation of mass:
;;;
Wherein, the The mass of the flow of the second working medium at the inlet of the second high-pressure turbine; the flow mass of the second working medium extracted from the second high-pressure turbine by the third mixer; the flow mass of the second working medium at the outlet of the second high-pressure turbine; The flow mass of the second working medium lost in the reheater; The flow mass of the second working medium at the outlet of the reheater; the flow mass of the second working medium extracted from the second low-pressure turbine by the second mixer; the flow mass of the second working medium extracted from the second low-pressure turbine by the first mixer; the flow mass of the second working medium at the outlet of the second low-pressure turbine.
In the embodiment provided with the steam extraction pipeline/steam extraction point, the pressure and the temperature of the steam extraction pipeline/steam extraction point need to be set, and the setting is selected according to the requirement of the outlet temperature.
In the embodiment of the invention, the first steam extraction pipeline is connected with the outlet of the second high-pressure turbine, and the second working medium in the first steam extraction pipeline flows from the second high-pressure turbine to the third mixer. In practical application, a first steam extraction point is generally set on the third mixer, and the first steam extraction point is connected to the first steam extraction pipeline, so as to realize steam extraction operation. The parameter design of the extraction point is very important, and the parameter design can influence the energy distribution and the regenerative efficiency of the system, and the system load can be effectively balanced by controlling the fluid quality of the first extraction pipeline, so that the stable operation of the system is ensured.
In some preferred embodiments, the mass flow rate of the first extraction conduit is expressed as:
;
Wherein, the The mass flow of the second working medium is extracted; The enthalpy value changes before and after the steam extraction of the first steam extraction point; The mass flow of the second working medium at the inlet of the second high-pressure turbine; Is the enthalpy value of the second working medium when flowing out of the third mixer, Is the enthalpy value of the second working medium flowing into the third mixer.
In the scheme, based on the law of conservation of energy, the mass flow of the inlet of the first steam extraction pipeline is solved through the known mass flow and enthalpy parameters, so that the influence of the change of the heat capacity flow rate on the system parameters can be effectively and fully considered.
The second extraction pipeline is connected with the second low-pressure turbine and the second mixer, and the second working medium in the second extraction pipeline flows from the second low-pressure turbine to the second mixer. In practical application, a second steam extraction point is generally set on the second mixer, and the second steam extraction point is connected to a second steam extraction pipeline, so as to realize steam extraction operation.
In some preferred embodiments, the mass flow rate of the second extraction conduit is expressed as:
;
Wherein, the The mass of the second working medium at the outlet of the second low-pressure turbine; And Enthalpy values of a second working medium at an inlet and an outlet of the second mixer respectively; The mass flow of the second working medium extracted for the second extraction point; The enthalpy value changes before and after the steam extraction of the second steam extraction point.
The third steam extraction pipeline is connected with the second low-pressure turbine and the first mixer, and the second working medium in the third steam extraction pipeline flows from the second low-pressure turbine to the first mixer. In practical application, a third steam extraction point is generally set on the second mixer, and the third steam extraction point is connected to a third steam extraction pipeline, so as to realize steam extraction operation.
In some preferred embodiments, the mass flow rate of the inlet of the third extraction conduit is expressed as:
;
Wherein, the The enthalpy value of the second working medium at the inlet of the first mixer; The mass flow of the second working medium extracted for the third extraction point; The enthalpy value changes before and after the steam extraction of the third steam extraction point.
When the model parameters are optimized, the efficiency, the power and the like of the system are required to be calculated so as to realize accurate optimization.
Because losses must be realized during the expansion of the turbine unit and the compression of the working medium by the power unit, the thermal efficiency of the pump is expressed as:
;
Wherein, the The actual work done for the pump to the working medium of unit mass includes various losses inside the pump; isentropic work is performed assuming that the compression process within the pump is an isentropic process; The actual enthalpy value of the working medium at the inlet of the pump; ideal enthalpy value in isentropic process for pump inlet; is the ideal enthalpy value of the pump outlet in the isentropic process.
It will be appreciated that the power of the pumpThe enthalpy value of the second working medium at the inlet and the outlet is calculated based on the enthalpy value of the second working medium, and the enthalpy value is expressed as follows:
;
;
;
Wherein, the Is the total power of the system; for a second high pressure turbine power; For a second low pressure turbine power; Is the conventional lost power; Is pump power; is the second generator efficiency; is the heat consumption rate; heat is consumed for the system; the flow mass of the second working medium in the system; Is the enthalpy loss of the second working medium.
In order to provide better thermal performance of the condenser in condensing the working fluid, the condenser pressure cannot be selected to be the saturation pressure because if the condenser pressure is too low, the humidity of the final stage turbine will increase, which will reduce the life and efficiency of the turbine. The calculation of the condenser parameters can be expressed as:
;
Wherein, the The mass of the second working medium in the condenser; is the enthalpy of the steam as it enters the condenser; Mass flow of cooling water in the condenser; is the enthalpy value of the cooling water when entering the condenser; is the enthalpy of the steam as it leaves the condenser; is the enthalpy of the cooling water as it leaves the condenser.
It should be noted that the reheat stage arrangement can also enhance the thermal performance of the coupled thermodynamic cycle system.
It is found through verification that, compared with the traditional thermodynamic cycle system for a fusion reactor, the isentropic efficiency of the second turbine unit in the organic Rankine cycle module is improved from 0.85 to 0.92, and as the isentropic efficiency of the turbine is improved, the net work of the system is increased from 77.64 kilowatts to 82.23 kilowatts, and the heat extracted by the condenser is reduced from 216.1 kilowatts to 211.5 kilowatts. It can be seen that by employing embodiments of the present invention, thermal performance of thermodynamic cycle systems can be effectively improved from many aspects.
Those skilled in the art will appreciate that implementing all or part of the above-described methods in accordance with the embodiments may be accomplished by way of a computer program stored on a computer readable storage medium, which when executed may comprise the steps of the embodiments of the methods described above. The storage medium may be a magnetic disk, an optical disk, a Read-Only Memory (ROM), a random-access Memory (Random Access Memory, RAM), or the like.
While the foregoing is directed to the preferred embodiments of the present invention, it will be appreciated by those skilled in the art that changes and modifications may be made without departing from the principles of the invention, such changes and modifications are also intended to be within the scope of the invention.
Claims (7)
1. The coupled thermodynamic cycle system is characterized by comprising a Brayton cycle module, a heat exchanger module and an organic Rankine cycle module with a reheating stage, wherein the heat exchanger module comprises a first channel and a second channel;
The working medium of the Brayton cycle module is a first working medium, and the working medium of the organic Rankine cycle module is an organic second working medium;
the Brayton cycle module is connected with the heat source and used for converting heat energy transferred by the heat source into first electric energy; the inlet of the first channel sucks a first working medium expanded by the Brayton cycle module, the inlet of the second channel sucks a second working medium deoxidized by the organic Rankine cycle module, and the outlet of the first channel and the outlet of the second channel respectively return the first working medium and the second working medium after heat exchange to the Brayton cycle module and the organic Rankine cycle module;
The brayton cycle module comprises a first turbine unit, a regenerator, a cooler unit, a compressor unit and a first generator;
The heat source is connected with the inlet of the first turbine unit, the outlet of the first turbine unit is connected with the inlet of the heat regenerator, the first generator and the inlet of the first channel, the first outlet of the heat regenerator is connected with the heat source, the second outlet of the heat regenerator is connected with the inlet of the compressor unit through the cooler unit, and the outlet of the compressor unit is connected with the heat regenerator and the inlet of the first turbine unit;
the first turbine unit comprises a first high-pressure turbine and a first low-pressure turbine which are sequentially connected, wherein the inlet of the first high-pressure turbine is the inlet of the first turbine unit, and the outlet of the first low-pressure turbine is the outlet of the first turbine unit;
The organic Rankine cycle module comprises a second turbine unit, a reheater, a condenser, a deaerator, a mixer unit, a steam extraction pipeline unit and a second generator;
The second turbine unit comprises a second high-pressure turbine and a second low-pressure turbine, the mixer unit comprises a first mixer, a second mixer and a third mixer, and the steam extraction pipeline unit comprises a first steam extraction pipeline, a second steam extraction pipeline and a third steam extraction pipeline;
The outlet of the second channel is connected with the inlet of the second high-pressure turbine, the outlet of the second high-pressure turbine is connected with the inlet of the second low-pressure turbine and the inlet of the reheater, the outlet of the reheater is connected with the inlet of the second low-pressure turbine, the outlet of the second low-pressure turbine is connected with the inlet of the first mixer, the outlet of the first mixer is connected with the second mixer, the outlet of the second mixer is connected with the inlet of the first mixer, the outlet of the second mixer is connected with the inlet of the deaerator, the outlet of the deaerator is connected with the inlet of the third mixer, the outlet of the third mixer is connected with the inlet of the deaerator and the inlet of the second channel, the first steam extraction pipeline connects the second high-pressure turbine with the third mixer and the reheater, the second steam extraction pipeline connects the second low-pressure turbine with the first mixer, and the third steam extraction pipeline connects the second low-pressure turbine with the second mixer.
2. The coupled thermodynamic cycle system of claim 1, wherein the first working fluid is supercritical carbon dioxide and the second working fluid is R245fa.
3. The coupled thermodynamic cycle system of claim 1, wherein the first working fluid sequentially passes through the compressor unit, the first turbine unit, the regenerator, the cooler unit, and then is introduced into the compressor unit to form a cycle, and the first working fluid output through the outlet of the first channel sequentially passes through the regenerator and the cooler unit and is introduced into the compressor unit.
4. The coupled thermodynamic cycle system of claim 1, wherein the compressor unit includes a cooler and a plurality of compressors connected in sequence, and wherein a cooler is further disposed between adjacent compressors.
5. The coupled thermodynamic cycle system of claim 1, wherein the second working fluid sequentially passes through the deaerator, the third mixer, the heat exchanger module, the second high pressure turbine, the reheater, the second low pressure turbine, the condenser, the first mixer, and the second mixer, and is circulated by passing through the deaerator, wherein the second working fluid further passes through the second high pressure turbine to enter the third mixer and the reheater, and wherein the second working fluid further passes through the second low pressure turbine to be respectively passed through the first mixer and the second mixer.
6. The coupled thermodynamic cycle system of claim 1, wherein the organic Rankine cycle module further comprises a power unit comprising a first pump and a second pump, wherein the second working fluid enters the organic Rankine cycle module through the power unit;
the first pump is arranged between the outlet of the condenser and the inlet of the first mixer, and the second pump is arranged between the outlet of the deaerator and the inlet of the third mixer.
7. The coupled thermodynamic cycle system of claim 1, wherein the organic rankine cycle module further comprises a valve unit including a first valve, a second valve, a third valve, and a fourth valve;
The first valve is arranged between the outlet of the second channel and the inlet of the second high-pressure turbine, the second valve is arranged between the outlet of the second mixer and the inlet of the first mixer, the third valve is arranged between the outlet of the third mixer and the inlet of the deaerator, and the fourth valve is arranged between the outlet of the third mixer and the inlet of the second channel.
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